WO2009085565A1 - Methods of converting methanol feedstock to olefins - Google Patents
Methods of converting methanol feedstock to olefins Download PDFInfo
- Publication number
- WO2009085565A1 WO2009085565A1 PCT/US2008/085791 US2008085791W WO2009085565A1 WO 2009085565 A1 WO2009085565 A1 WO 2009085565A1 US 2008085791 W US2008085791 W US 2008085791W WO 2009085565 A1 WO2009085565 A1 WO 2009085565A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- dme
- water
- methanol
- olefins
- oxygenates
- Prior art date
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
- C07C1/20—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C11/00—Aliphatic unsaturated hydrocarbons
- C07C11/02—Alkenes
- C07C11/06—Propene
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C11/00—Aliphatic unsaturated hydrocarbons
- C07C11/02—Alkenes
- C07C11/08—Alkenes with four carbon atoms
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C41/00—Preparation of ethers; Preparation of compounds having groups, groups or groups
- C07C41/01—Preparation of ethers
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C41/00—Preparation of ethers; Preparation of compounds having groups, groups or groups
- C07C41/01—Preparation of ethers
- C07C41/09—Preparation of ethers by dehydration of compounds containing hydroxy groups
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/11—Purification; Separation; Use of additives by absorption, i.e. purification or separation of gaseous hydrocarbons with the aid of liquids
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2529/00—Catalysts comprising molecular sieves
- C07C2529/82—Phosphates
- C07C2529/84—Aluminophosphates containing other elements, e.g. metals, boron
- C07C2529/85—Silicoaluminophosphates (SAPO compounds)
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/40—Ethylene production
Definitions
- This disclosure relates to methods of converting methanol feedstock to olefins.
- Methanol is produced in large quantities throughout the world and is available as a feedstock for olefins. Also, methane and synthesis gas are often times available for use as a feedstock for olefin production. Moreover, there is an increasing demand for environmentally friendly processes which are capable of minimizing reaction by-products that are not capable of being recycled or used in other capacities.
- FIGURE is a schematic representation of one representative example of a system that can be employed to produce olefins.
- FIGURE is a simplified schematic process flow diagram for a process scheme, generally designated by the reference numeral 10, for the production of olefins from methanol.
- process scheme generally designated by the reference numeral 10
- FIGURE is a simplified schematic process flow diagram for a process scheme, generally designated by the reference numeral 10.
- a hydrocarbon or carbonaceous feedstream 12 may comprise a variety of materials, including but not limited to natural gas (mostly methane and ethane), refinery residues, coal and the like and can be processed by conventional means in a synthesis gas production zone 14 such as by steam reformation, partial oxidation, auto thermal reformation and the like to provide a synthesis gas stream 16.
- Such a synthesis gas stream 16 can in turn be introduced into a synthesis gas conversion reactor zone 18 for contact with catalyst material and at reaction conditions effective to produce a synthesis gas conversion reactor zone effluent that includes dimethyl ether, other synthesis gas conversion products, such as methanol and water and unreacted synthesis gas.
- the synthesis gas conversion reaction zone effluent 20 can be appropriately separated in a separator 22 to form a stream 24 of dimethyl ether and a stream 26 of methanol.
- a feed such as generally composed of at least a portion of the separated product methanol can then be contacted in an oxygenate conversion reactor zone with an oxygenate conversion catalyst and at reaction conditions effective to convert the feed to an oxygenate conversion product stream comprising light olefins as discussed below.
- the synthesis gas production zone 14 can operate at conventional operating conditions such as at a reaction temperature ranging from 800 0 C to 950 0 C, a pressure ranging from 965 kPa to 2896 kPa, and a water to carbon molar ratio ranging from 2.0 to 3.5.
- impurities such as sulfur compounds, nitrogen compounds, particulate matter, and condensibles may be removed in a conventional manner (not shown) to provide the synthesis gas stream 16.
- the synthesis gas stream 16 is passed to the synthesis gas conversion reactor zone 18.
- oxygenates such as dimethyl ether (exiting as stream 24) and alcohols (exiting as stream 26) at conditions including a reactor temperature in the range of 150 0 C to 450 0 C at a pressure typically in the range of 69 kPa to 103,425 kPa over a variety of known catalysts such as a mixed metal oxide catalyst of CuO and ZnO, as one example.
- methanol is preferred.
- the methanol stream 26 is then fed to a first conversion reactor zone 28.
- the methanol fed into the first conversion reactor zone produces a conversion reactor zone effluent which comprises dimethyl ether, unreacted methanol and water, for example.
- the first reactor zone 28 operates under conditions effective to convert methanol to dimethyl ether under conditions including a reactor temperature in the range of 200 0 C to 300 0 C and a pressure of 345 kPa to 1034 kPa. Broader temperature and pressure ranges are possible under selected circumstances.
- the first conversion reactor zone 28 is preferably a fixed bed reactor containing gamma alumina catalysts with a surface area greater than 80 m 2 /gm. Other surface areas may be employed that are less than 80 m /gm under varying conditions. Also, there are other acidic catalysts, in addition to gamma alumina, that may be employed as desired.
- the first conversion reactor zone effluent stream 30 connects to a separation zone 32.
- the first conversion reactor zone effluent stream 30 entering the separation zone 32 is separated , typically by cooling, at a temperature from 300 0 C to 40 0 C into a dimethyl ether vapor stream 34 and a separator effluent stream 36 which may contain water, methanol, liquid dimethyl ether and miscellaneous oxygenates.
- Such cooling may be accomplished through one or more heat exchangers in series to maximize heat recovery from the effluent stream 30. Heat energy recovered may be used to preheat the feed stream 26 to the conversion zone 28, or for any other streams as appropriate.
- Second conversion zone 40 can be any conversion type reactor known in the art that is capable of converting dimethyl ether to light olefins.
- the temperature in the second conversion zone 40 can be 300 0 C to 600 0 C, although temperatures lower and higher may be employed as desired.
- pressures of 69 kPa to 690 kPa may be employed, although other pressures may also be used.
- Any number of catalysts may be employed in the second conversion zone 40. However, a fluidized bed reactor containing a SAPO catalyst is preferred. S APO-34 is particularly a preferred catalyst.
- a second conversion reactor zone effluent stream 42 exits second conversion reactor 40 and is passed through one or more heat exchangers in series to maximize heat recovery from stream 42 by cooling the second conversion zone 40 effluent from 450 0 C to 150 0 C.
- the separator 44 is a combination separation quench cooling tower. In separator 44 light olefins and unreacted dimethyl ether are separated from other components in the second conversion reactor zone effluent stream 42 and exit as an effluent stream 46. The separator 44 also produces an effluent stream 48 that includes water and various oxygenates.
- the effluent stream 46 is then passed to a compressor 50 which compresses the effluent stream 46. Compression typically depends on the actual stream composition and on the fractionation scheme. If a demethanizer is required, compression may be up to 3.2 or 3.5 MPa. If neither a demethanizer nor an acetylene converter is required, the compressor discharge pressure may be dropped to 2 MPa. hi some situations, it is possible and may be more economical to first compress to the pressure necessary for the DME absorber and then further compress the gaseous effluent to the pressure required for the olefin separation train.
- the compressed stream 52 enters absorber 54 which operates at a temperature of 30 0 C to 100 0 C and at a pressure of 690 kPa to 2758 kPa. Although these are preferred temperatures and pressures, other temperatures and pressures may be employed to suit operating conditions.
- the absorbing liquid may be any number of absorbing liquids known in the art. However, water or a water/methanol mixture passed through a gas liquid absorber in a counter-current flow is particularly preferred.
- Absorber 54 produces a light olefin effluent stream 56 and a recycle effluent stream 58 including absorber fluid, dimethyl ether, various oxygenates, various hydrocarbons and water.
- the olefin effluent stream 56 which typically includes ethylene, propylene and/or butylene may then be sent to a conventional fractionation to recover individual pure component products, such as ethylene and propylene which could be channeled to any other use typically known in the art such as, for example, the production of polyolefins such as polyethylene, polypropylene and the like.
- At least portions of the effluent stream 36 from separator 32 which comprises a first aqueous stream, the effluent stream 48 from separator 44 which comprises a second aqueous stream and the effluent stream 58 from absorber 54 which comprises a third aqueous stream may be combined into a recycle effluent stream 60 which is sent to a stripper 62.
- Stripper 62 produces a purified water effluent stream 64 which comprises a fourth aqueous stream, at least a portion of which may be recycled as an absorber fluid to the absorber 54 or used for completely different uses, including further treatment for use in other processes.
- Stripper 62 also produces a stream 68 essentially containing methanol DME and possibly other light hydrocarbons.
- Recycle stream 68 may be recycled to conversion zone 28 and/or the conversion zone 40 to maximize light olefins production. It is preferred to recycle the methanol to conversion zone 28 and to recycle the DME to conversion zone 40.
- a portion of water effluent stream 64 may be used as an absorbing fluid in absorber 54 by way of line 74.
Abstract
Description
Claims
Priority Applications (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
MX2010005886A MX2010005886A (en) | 2007-12-21 | 2008-12-08 | Methods of converting methanol feedstock to olefins. |
RU2010130313/04A RU2487856C2 (en) | 2007-12-21 | 2008-12-08 | Method of converting methanol material to olefins |
AU2008343505A AU2008343505B2 (en) | 2007-12-21 | 2008-12-08 | Methods of converting methanol feedstock to olefins |
CN200880122325XA CN101903311B (en) | 2007-12-21 | 2008-12-08 | Methods of converting methanol feedstock to olefins |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US12/004,843 US7919660B2 (en) | 2007-12-21 | 2007-12-21 | Methods of converting methanol feedstock to olefins |
US12/004,843 | 2007-12-21 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2009085565A1 true WO2009085565A1 (en) | 2009-07-09 |
Family
ID=40789429
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/US2008/085791 WO2009085565A1 (en) | 2007-12-21 | 2008-12-08 | Methods of converting methanol feedstock to olefins |
Country Status (8)
Country | Link |
---|---|
US (1) | US7919660B2 (en) |
CN (1) | CN101903311B (en) |
AU (1) | AU2008343505B2 (en) |
CL (1) | CL2008003791A1 (en) |
MX (1) | MX2010005886A (en) |
MY (1) | MY151106A (en) |
RU (1) | RU2487856C2 (en) |
WO (1) | WO2009085565A1 (en) |
Cited By (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2014067955A1 (en) * | 2012-10-31 | 2014-05-08 | Shell Internationale Research Maatschappij B.V. | Processes for the preparation of an olefinic product |
WO2014067958A1 (en) * | 2012-10-31 | 2014-05-08 | Shell Internationale Research Maatschappij B.V. | Processes for the preparation of an olefinic product |
WO2014067957A1 (en) * | 2012-10-31 | 2014-05-08 | Shell Internationale Research Maatschappij B.V. | Processes for the preparation of an olefinic product |
WO2014067967A1 (en) * | 2012-10-31 | 2014-05-08 | Shell Internationale Research Maatschappij B.V. | Process for removing oxygenates from an olefin stream |
Families Citing this family (10)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US8003841B2 (en) * | 2008-06-30 | 2011-08-23 | Uop Llc | Integration of OTO process with direct DME synthesis |
US8686206B2 (en) * | 2010-11-09 | 2014-04-01 | Primus Green Energy Inc. | Single loop multistage fuel production |
US20130178676A1 (en) * | 2012-01-05 | 2013-07-11 | Uop Llc | Methods for producing light olefins |
DE102012215757A1 (en) * | 2012-09-05 | 2014-03-06 | Evonik Industries Ag | Process for the preparation of linear butenes from methanol |
DE102013101575B4 (en) | 2012-12-21 | 2019-06-06 | L’AIR LIQUIDE Société Anonyme pour l’Etude et l’Exploitation des Procédés Georges Claude | Process and plant for the production of olefins from oxygenates |
US9670416B2 (en) | 2014-12-10 | 2017-06-06 | Primus Green Energy Inc. | Configuration in single-loop synfuel generation |
CN105523876B (en) * | 2015-12-17 | 2017-08-25 | 神华集团有限责任公司 | A kind of method by preparing propylene from methanol |
CN109833905A (en) | 2017-11-29 | 2019-06-04 | 中国科学院大连化学物理研究所 | Molecular sieve catalyst and its preparation method and application |
US10647623B2 (en) | 2018-08-10 | 2020-05-12 | Uop Llc | Processes for reduced oxygenated recycle in an MTO conversion |
CN114531875B (en) * | 2019-05-20 | 2024-03-26 | 沙特基础工业全球技术公司 | On-line process for treating waxy crude methanol stream |
Citations (5)
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US5191142A (en) * | 1991-12-23 | 1993-03-02 | Amoco Corporation | Process for converting methanol to olefins or gasoline |
US5573990A (en) * | 1992-05-03 | 1996-11-12 | Dalian Institute Of Chemical Physics | Process for the conversion of methanol to light olefins and catalyst for such process |
WO2001021561A1 (en) * | 1999-09-23 | 2001-03-29 | Mobil Oil Corporation | Process for converting methanol or dimethyl ether to olefins |
US20040215043A1 (en) * | 2003-04-22 | 2004-10-28 | Senetar John J. | Selective dimethylether recover and recycle in a methanol-to-olefin process |
JP2007063270A (en) * | 2005-08-15 | 2007-03-15 | China Petrochemical Corp | Method for producing lower olefin from methanol or dimethyl ether |
Family Cites Families (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE10117248A1 (en) * | 2000-05-31 | 2002-10-10 | Mg Technologies Ag | Process for producing propylene from methanol |
CN1156416C (en) * | 2001-12-14 | 2004-07-07 | 清华大学 | Process and system for preparing low-carbon olefin from methanol or dimethylether |
KR100501922B1 (en) * | 2003-02-19 | 2005-07-18 | 에스케이 주식회사 | Process for preparing dimethyl ether from methanol |
US20060020155A1 (en) * | 2004-07-21 | 2006-01-26 | Beech James H Jr | Processes for converting oxygenates to olefins at reduced volumetric flow rates |
-
2007
- 2007-12-21 US US12/004,843 patent/US7919660B2/en active Active
-
2008
- 2008-12-08 MX MX2010005886A patent/MX2010005886A/en active IP Right Grant
- 2008-12-08 AU AU2008343505A patent/AU2008343505B2/en not_active Ceased
- 2008-12-08 WO PCT/US2008/085791 patent/WO2009085565A1/en active Application Filing
- 2008-12-08 MY MYPI20102415 patent/MY151106A/en unknown
- 2008-12-08 CN CN200880122325XA patent/CN101903311B/en active Active
- 2008-12-08 RU RU2010130313/04A patent/RU2487856C2/en not_active IP Right Cessation
- 2008-12-18 CL CL2008003791A patent/CL2008003791A1/en unknown
Patent Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US5191142A (en) * | 1991-12-23 | 1993-03-02 | Amoco Corporation | Process for converting methanol to olefins or gasoline |
US5573990A (en) * | 1992-05-03 | 1996-11-12 | Dalian Institute Of Chemical Physics | Process for the conversion of methanol to light olefins and catalyst for such process |
WO2001021561A1 (en) * | 1999-09-23 | 2001-03-29 | Mobil Oil Corporation | Process for converting methanol or dimethyl ether to olefins |
US20040215043A1 (en) * | 2003-04-22 | 2004-10-28 | Senetar John J. | Selective dimethylether recover and recycle in a methanol-to-olefin process |
JP2007063270A (en) * | 2005-08-15 | 2007-03-15 | China Petrochemical Corp | Method for producing lower olefin from methanol or dimethyl ether |
Cited By (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2014067955A1 (en) * | 2012-10-31 | 2014-05-08 | Shell Internationale Research Maatschappij B.V. | Processes for the preparation of an olefinic product |
WO2014067958A1 (en) * | 2012-10-31 | 2014-05-08 | Shell Internationale Research Maatschappij B.V. | Processes for the preparation of an olefinic product |
WO2014067957A1 (en) * | 2012-10-31 | 2014-05-08 | Shell Internationale Research Maatschappij B.V. | Processes for the preparation of an olefinic product |
WO2014067967A1 (en) * | 2012-10-31 | 2014-05-08 | Shell Internationale Research Maatschappij B.V. | Process for removing oxygenates from an olefin stream |
US9828306B2 (en) | 2012-10-31 | 2017-11-28 | Shell Oil Company | Processes for the preparation of an olefinic product |
US9828312B2 (en) | 2012-10-31 | 2017-11-28 | Shell Oil Company | Process for removing oxygenates from an olefin stream |
US9828305B2 (en) | 2012-10-31 | 2017-11-28 | Shell Oil Company | Processes for the preparation of an olefinic product |
US9834488B2 (en) | 2012-10-31 | 2017-12-05 | Shell Oil Company | Processes for the preparation of an olefinic product |
Also Published As
Publication number | Publication date |
---|---|
AU2008343505B2 (en) | 2013-01-17 |
RU2487856C2 (en) | 2013-07-20 |
CL2008003791A1 (en) | 2009-10-09 |
RU2010130313A (en) | 2012-01-27 |
US20090163751A1 (en) | 2009-06-25 |
AU2008343505A1 (en) | 2009-07-09 |
CN101903311A (en) | 2010-12-01 |
MY151106A (en) | 2014-04-15 |
US7919660B2 (en) | 2011-04-05 |
MX2010005886A (en) | 2010-10-05 |
CN101903311B (en) | 2013-08-14 |
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